Control system



June 16, 1942. .1 F LUHRs 2,286,863

CONTROL SYSTEM Fiedsept. 5, 1940 5 sheets-sheet 1 INVENTOR BY ff ...J LOM ATTOR Y June 16, 1942. J. F. LUI-ms CONTROL SYSTEM 5 Sheets-Sheet 2 INVENTOR Filed Sept.

June 1,6, 1942. J, F UHRS 2,286,863

CONTROL SYSTEM Filed sept. 5, i940 5 sheetsl-*sheet 5 INVENTOR JOHN f.' UH/2s BY Tm/ogn June 16, 1942. J. F. LuHRs I 2,286,863

CONTROL SYSTEM Filed sept. 5, 1940 5 sheets-sheet 4 nventor JOHN F. LUHRS VWM June 16, 1942. J. F; LuHRs coNTRo'Ll SYSTEM Filed sept. 5, 1940 5 Sheets-Sheet 5 Snventor JOHN F. LUHRS attonug Patented June 16, 1942 CONTROL SYSTEM John F. Luhrs, Cleveland Heights, Ohio, assignor to Bailey Meter Company, a corporation of Delaware Application September 5, 1940, Serial No. 355,446

23 Claims.`

This invention relates to the art of measuring and/or controlling the magnitude of a variable quantity, condition, relation, etc., and particularly such a variable condition as the density of a liquid-vapor mixture, although the variable might be temperature, pressure or any physical, chemical, electrical, hydraulic, thermal or other characteristic.

I have chosen to illustrate and describe as a preferred embodiment of my invention its adaptation to the measuring and controlling of the lensity and other characteristics of a owing seated fluid stream, such as the flow of hydrocarbon oil through a cracking still.

While a partially satisfactory control of the cracking operation may be had from a knowled-ge of the temperature, pressure and rate of flow of the fluid stream being treated, yet a knowledge of the density of the owing stream at different points in its path is of a considerably greater value to the operator, but was not available prior to the discovery by Robert L. Rude, as claimed in his copending application Serial No. 152,860 filed July 9, 1937, now Patent No. 2,217,634 dated October 8, 1940.

In the treatment of water below the critical pressure, as in a vapor generator, a knowledge of temperature, pressure and rate of flow may be suicient `for proper control, inasmuch as deflnite tables have been established for interrelation between temperature and pressure and from which tables the density of the liquid or vapor may be determined. However, there are no available tables for mixtures of liquid and vapor.

In the processing of a fluid, such as a petroleum hydrocarbon, a change in density of the uid may occur through at least three causes:

l. The generation or formation of vapor of the liquid, whether or not separation from the liquid occurs.

2. Liberation of dissolved or entrained gases.

3. Molecular rearrangement as by cracking or polymerization.

The result is that no temperature-pressuredensity tables maybe established for any liquid, vapor, or liquid-vapor condition of such a fluid, and it is only through actual measurement of the density of a mixture of the liquid and vapor that the operator may have any reliable knowledge as to thephysical condition of the fluid stream at various points in its treatment.

It will be readily apparent to those skilled in the art that the continuous determination of the density of such a flowing stream is of tremendous importance and value'to an operator in controlling the heating, mean density, time of detention in a given portion of the circuit, etc. A continuous knowledge of the density of such a heated owing stream is particularly advantageous where wide changes in density occur due to formation, generation, and/or liberation of gases, with a resulting formation of liquid-vapor mixtures, velocity changes, and Varying time of detention in different portions of the fluid path. In fact, for a fixed or given volume of path, a determination of the mean density in that portion provides the only possibility of accurately determining the time that the fluid in that lportion of the path is subjected to heating or treatment. By my invention I provide the requisite system and apparatus wherein such information is made available continuously to an operator, and furthermore may comprise the guiding means for automatic control of the process or treatment.

While illustrating and describing my invention as preferably adapted to the cracking of petroleum hydrocarbon, it is to be understood that it may be equally adaptable to the vaporization or treatment of other liquids and in other processes.

In the drawings: l

Fig. 1 is a diagrammatic representation of density measuring apparatus for a heated fluid stream.

Fig. 2 is similar to Fig. 1 but includes a determination of mean density.

Fig. 3 is a diagrammatic arrangement of the invention in connection with a heated fluid stream.

Figs, 4, 5 and 6 are simplified wiring diagrams of the composite wiring of Fig. 3.

Fig. 'I is a diagrammatic arrangement similar to Fig. 2 but showing certain modications thereof.

Fig. 8 illustrates in diagrammatic manner a composite of Figs. 2 and 3 including automatic control provisions.

Referring now in particular to Fig. 1, I indicate a conduit I which may be considered as comprising the once through fluid path of an oil still wherein a portion of the path is heated as by a burner 2. The rate of flow of the charge or relatively untreated hydrocarbon is continuously measured by the rate of flow meter or differential recorder 3, while a differential recorder 4 is located with reference to the -conduit l beyond the heating means or after the flowing fluid has been subjected to heating or other processing.

The float actuated meter 3 is Sensitive to the differential pressure across an obstruction such as an orifice, flow nozzle, Venturi tube, or the like, positioned in the conduit for effecting a temporary increase in the Velocity of the flowing iiuid. Such an orifice may be inserted in the conduit between fianges as at 5. The meter 3 is connected by pipes 6, 'l to opposite sides of the orifice 5 and comprises a liquid sealed U-tube, in one leg of which is a float operatively connected to position an indicator 8 relative to an index S. In similar manner the indicator I of the meter 4 is positioned relative to an index I I; the meter 4 being responsive to the differential head across an orifice or similar restriction be.- tween the flanges I2.

The relation between volume fiow rate and differential pressure (head) is:

Q=QM\/2yh (1) where Q=cu. ft per sec. C--coefiicient of discharge M=meter constant (depends on pipe diameter and diameter of orifice hole) `qracceleration of gravity=32.17 ft. per sec. per

sec.

h=differential head in ft. of the flowing fluid The coefcient of discharge remains substantially constant for'any one ratio of`orice diameter to pipe diameter, regardless ofthe density or specific volume of the fiuid being measured. With C, M, and \/*2g all remaining constant, then Q varies as the vh. Thus it will be seen that the float rise of the meters 3, 4 is independent of variation in densityV or specific volume of the fluid at the two points of measurement and that the reading on the indexes 9, II of differential head is directly indicative of volume flow. If the conduit size and orifice hole size are the same at both meter locations, then the relation of meter readings is indicative of the relation of density and specific volume.

This may readily be seen, for if it were desired to measure the flowing fiuicl in units of weight, Formula 1 becomes:

where W=rate of flow in pounds per sec.

d=density in pounds per cu. ft. of the flowing fluid.

hxdifferential head in inches of a standard liquid such as water Mzmeter constant now including a correction to bring h of Equation l into terms of h of Equation 2.

Assuming the Same weight rate of fiow passing successively through two similar spaced orifices 5, I2 and with a change in density as may be caused by the heating means 2, then the density at the second orifice I2 may be determined as follows:

W1 2=VV5 1/2gh12d12 1/2gh5d5 windu i/hd ds=d 25 3) 12 Thus it will be observed that, knowing the density of the fluid passing the orifice 5 I may readily determine the density of the fluid passing the orifice I2, from the relation of differential pressures indicated by the meters 3, 4.

Referring now to Fig. 2, wherein like parts bear the same reference numerals as in Fig. 1, I indicate that after the fluid has passed through the orice I 2A it is returned to a further heating section of the still, from which it passes through a third differential pressure producing orifice I3A. The heating coil I4 will be hereinafter referred to as a first heating section, while the coil I5 will be referred to as a second heating section. In the preferred arrangement and operation of the still the section I 5 is the conversion or cracking section, and the one in which it is primarily desirable to" continuously determine the mean density of the fluid, as well as its time of detention or'treatment in this section. For that reason I now desirably determine the mean density of the fluid in the section I5 and accomplish this through an interrelation of the differential pressures produced by theV same weight'fiow passf ing successively' through the orifices 5, IZA, I3A. The same total weight of lfluid must pass through the three orifices in succession'so long as there is no addition to or diversion from the path'intermediate the orifices. It is'equally apparent that in the heating of a petroleum hydrocarbon, as by the coil'llzbetween the orifices 5 and IZA, there will be a .changev in density o f the 'fiuid between the two orifices, and furthermore that an additional heating of the fluid, as by the coil I5, will further vary the density of the fluid as at the orifice I3A relative to-the orifice 12A.

Assume now that the conduit I is of a uniform size throughout and that the orifices 5, I2'A and ISA are of a uniform opening area and coefficient or characteristic. Through:V the agency of the meter I6 the differential pressure existing across the orifice v18A is continuously indicated upon an index I8 by an'indica'tor Itl. The mean density of the fluid in theconversion section I5 is then obtained by averaging the density. of the fluid at the orifices IZ'A,` I3A. As for example:

d d mdlF-z (4) his/1 2 5) Thus the mean density of the flowing fluid in the conversion section I5 (knowing the density or specific gravity of the uid entering the sysm tem) may be directly computed from the readings of the indexes 9 II, I8. This, of course, on the basis that the orifices 5, I 2A, I? A are the same, and that the capacity of the fioat meters 3, 4 I6 is the same.

Now as the specific volume increases progressively from locations 5 to Il A to I `3A the differential pressure across these orifices increases in like manner, and in the operation of such a cracking still it may be that the differential pressure across an orifice I3 A will be several times that across the orifice 5 if the orifice sizes are equal. I have therefore indicated at IZA,` 13A of Fig. 2 that these orifices may be of. an adjustable type wherein the ratiol of orifice hole to pipe alea may be varied externally of the conduit through suitable hand wheel or other means. The actual orifice design in terms of pounds per c=coeflicient of discharge f=factor of approach sp. vol.='cu. ft./1b.

Now considering that orifice IZA is so adjusted that its cD2 is different from that of orce 5, I may then determine the density at I2A as fol lows:

d12A=CR2 where D 2 c=d (of 5 CfDzA R=fi 1/ 1742A In similar manner I may determine the density at the orice I3A regardless of the orifice area, so long as I take into account the cfD2 of the orice vin the above manner. It will thus be seen that if the specific volume of the owing iiuid increases so rapidly that the differential head at successive orifice locations (for the same design of orifice) becomes many times the value of the differential head at the initial orifice, it would be impractical to attempt to indicate orrecord such differential head relative to a single index or record chart without one or more of the indications or records going beyond the capacity of the index or chart. There are two ready means of overcoming this practical difficulty, the first being an adjustment of the successive orifices, such as I2A, I3A to have new values of cfD2 such that the indicator or recording pen will be kept on the chart; and the second through varying the basic capacity of the meter 4 or IG relative to the meter 3. This latter method is accomplished by so arranging the meter 4, for example, that it requires 50% greater differential pressure to move the related pointer over full index range than in the case of meter 3. This may readily be accomplished by properly proportioning the two legs of the mercury U-tube, on one of which the oat is carried. Of course it will be necessary to take such changes in capacity into account when utilizing the differential head readings in determining density or mean density.

For example, the reading of the pointer relative to the index should be on a percentage basis of whatever maximum head the meter is designed for. 'Ihen the total head corresponding to the indicator reading will be available or the proper correction may be applied. .Assume that the meter U-tube 3 is so shaped that it requires 120 water differential applied thereto to move the indicator 8 from Zero to 100% travel over the index 9, and that for meters 4 and I6 it requires 250" water differential to cause the indicator I0 to move from zero to 100% over the index II, and I1 relative to I8. Then:

Y Y F3` float travel of meter 3 F4=% iioat travel of meter 4 In Fig. 3 I show in diagrammatic fashion an arrangement similar to that of Fig. 2, but adapted to give further indications valuable as a guide to operation of the system by manual or automatic means. Herein I illustrate mechanism under the control of the meters 3, 4, I6 for making directly and visually available the information I desire for the manual or automatic control of the cracking still.

In the operation of'such a cracking still it is of considerable importance to determine, in addition to the mean density, the time of detention of the fluid in various portions of the fluid flow path. It is also'of importance to determine the time-temperature relation of the conversion section. For example, the time that any particle remains in this section and the temperature to which it is subjected, or the temperature at which the mixture leaves the section. To determine such temperature I indicate in Fig. 2 at I9 the bulb of a gas-lled thermometer system of which 20 indicates the connecting capillaryand 2| a Bourdon tube whose free end is positioned responsive to the temperature at the bulb location.

According to Equation 5 it is necessary, in determining the mean density of the conversion section, to obtain the ratio of the differential heads at orifices 5 and I2A. Then to obtain the ratio of the differential heads at orifices 5 and ISA. To then average these ratios. My invention is based in general on the use of the Wheatstone bridge through whose agency ratios may be directly obtained. With such a system the meters 3, 4, 16 may with a minimum of work position a contact arm relative to a resistance forming an arm of a Wheatstone bridge. The system lends itself readily to the remote grouping of the apparatus necessary to indicate the individual values or relations and which I desirably locate convenient to the operator for hand or automatic control of the process.

The arm 8 of meter 3 is of insulating material but carries a conducting portion adapted to continuously contact a metallic segment 22 and to movably engage a rheostat 23 providing a resistance RC representative of the position of the float of` meter 3, or F3. A second conducting portion on the arm 8 contacts a metallic segment 24 and movably engages a rheostat 25 providing a resistance RCI. In similar manner the arm I0 provides a resistance RI representative of F4; and the arm I'I provides a resistance RO representative of F16.

Referring now to Fig. 4 it will be observed that the adjustable resistances RC and RI comprise two arms of a Wheatstone bridge. A third arm includes a hand adjustable resistance F, while a fourth arm includes a xed resistance FI and an adjustable resistance BI. The value of the resistance FI is substantially the same as of the resistance F. The resistance BI is known as the balancing resistance and is varied by movement of the arm 30 through the agency of the reversible synchronous motor 3| under control of a galvanometer 32.

The motor 3| is of the self-starting synchronous type of alternating curent motor and is shown as having normally energized opposed elds. Should the Wheatstone bridge become unbalanced, then the needle of the galvanometer 32 will move either clockwise or counterclockwise (Fig. 3), thereby open circuiting one of the fields of the motor 3|, resulting in a positioning of the arm 30 in direction and amount over the resistance BI to balance the bridge and cause the galvanometer needle to return to neutral position. It will be understood that the necessary gear reduction is to be incorporated between the motor 3| and the arm 30 so that the arm 30 moves at a relatively slow speed.

The Wheatstone bridge thus serves to continuously determine the density at IZA through solving Equation 8. Such density is continuously indicated on the index 33 and the value drzA is continuously represented by the resistances BI and BI I.

Solving Equations 3 and 8 Now RC r h5 RI 1 hizA RO OC hisA and it is expected that:

d d12A d1iiA h5 h12A h13A RC RI RO It is known that the law of the Wheatstone bridge is:

*RC *T El RC' or as lig RI and will tend to vary as the reciprocal of 0 to w.

In like manner the value of 0313A may be indicated on the index 34 and be continuously represented by the value of the resistance B2 I As clearly indicated the same power source 36 is alternatively used for both bridges. A motor 31 for the second bridge is under the control of a galvanometer 3B connected across the points 21, 35.

In the second bridge a hand adjustable resistance FF has substantially the same resistance value as F2. In fact under zero flow conditions the values of F, FI, FF, and F2 should be equal.

A time motor driven cam |00 continuously reciprocates a switch |0I alternately connecting the power source `36 into the two bridges. When either bridge is not connected to the power source 36 the galvanometer of that bridge remains at its neutral position and the various resistance values remain unchanged until the power source 3|; is again connected to that bridge.

It will now be observed that the resistance BI I is representative of the value 112A while the resistance B2I is representative of the value dm. To determine the mean density of the uid through the conversion section I5 (malls) I obtain the average of the ratios of heads (Equation 5) and accomplish this by including the resistance BI I and B2| in a third bridge circuit (Fig. 5). In this bridge circuit the value of the xed resistance A is twice that of the value of the xed resistance B. The adjustable resistance B3 is varied by the positioning of an arm 39, through the agency of a motor 40, under the control of a galvanometer 4I.

@JEH-PE21) but and

B3 =B11 -2i-B2l mdis The arm 39 will then indicate, relative to the index 46, the value of mis and the value of the resistance B3 will be representative of mis.

In designing the apparatus I incorporate an average expected value of specific gravity or density of the fluid at the orifice 5 in the resistance RC or the motion of the arm 8. Additionally I provide a hand adjusted rheostat II'I for taking care of variations in density of the ud at the orice 5 which may occur from time to time.

In similar fashion I design into the apparatus the expected value of cfD2 in connection with the resistance RI and also for the expected value of cfD2 in connection with the resistance RO. The auxiliary resistance F is moved by hand when a change in the cyD2 value for the orice |2A is made by the adjustable means provided. In the same manner, if the adjustable orifice |3A is moved to a new position and value of cfD2, the resistance FF is correspondingly varied. The resistances F, FF may be provided with indexes graduated to read in cfD2 values for the corresponding orice, or in fact they may be so connected as to be moved simultaneously by and with the means provided for moving the adjustable orifices. Reference to Fig. 7 will show that the stem of the adjustable orifice I2A is provided with an indicator |02 movable relative to an index |03 which may be graduated in cJD2 values; and that the stem also carries a contact movable along the resistance F. In like manner the arrangement in connection with the adjustable orifice I 3A is shown in Fig. 7. Thus at any time the position of an orifice |2A or |3A is varied, the necessary corresponding variation in the resistance value F or FF may be simultaneously accomplished.

The arm 8 is adapted to vary a resistance RCI proportional to V775 which so long as d5 remains constant equals W, where W is rate of now in pounds. This value is then included as an arm in a Wheatstone bridge circuit (Fig. including the resistance B3, the fixed resistance B, an equal xed resistance B4 and an adjustable resistance T, to determine the time of detention of any particle of fluid in the heating section l5.

TX=Time any particle is in section 15.

V=Volume between I2A and 13A (cu. ft.)

md=Rate of flow (lbs. per unit T) W=Rate of flow (lbs. per unit T) The resistance T is varied through movement of an arm 5I positioned by a motor 52, under the control of a galvanometer 53. An index 54 may be graduated to read directly in value of time of detention of any particle in the section l5. In order that the resistance RCI will represent the value of W or rate of flow in pounds per unit of time the risistance 25 is shaped according to the \/h5.

With the resistance T, is varied a resistance Tl, representative of time of detention, and this is incorporated in a bridge circuit (Fig. 6) in relation to a resistance TE, representative of value of temperature, positioned by the Bourdon tube 2l. The bridge circuit of Fig. 6 includes a resistance TT varied by an arm 59 moved by a motor 60, under the control of a galvanometer 6l for advising desired ratio or relation between time and temperature represented respectively by TI and TE. This relationship may be continuously recorded as at 62. Hand adjustable rheostats 63, 64 allow adjustment for constants of time and temperature as may become necessary.

In Fig. 7, previously referred to, the valve |04 in the fuel supply line 2 controls the heating, While the valve |05 in the conduit l controls the weight rate of iiow of fluid to be treated. Either or both of these valves may be manipulated by hand from indications of density, mean density, time of detention, time-temperature relation, or in fact from any of the indications previously referred to in connection with Figs. 1-7, inclusive.

In Fig. 8, I illustrate a composite of Figs. 2 and 3 in which the arms 30, 30', 5l, 39, or 59, each position an air pilot valve of the general type disclosed and claimed in the Johnson Patent No. 2,054,464 to establish an air loading pressure representative of density, mean` density, etc. In Fig. 8 the fuel control valve |06 and the flow control Valve |01 are spring loaded diaphragm-actuated valves responsive to any or all of the air loading pressures established by the pilot valves, through hand selecting valves 108 or |09, thus I may automatically control the flow and/or heating responsive to determined density or any of the variables mentioned.

While I have chosen tok illustrate and describe the functioning of my invention in connection with'the heating of petroleum or hydrocarbon oil, it is to be understood that the method and apparatus is equally applicable to the treatment, processing, or Working of other fluids, such for example, as in the vaporization of Water to form steam. l

This Vapplication constitutes a continuation-inpart of my application Serial No. 152,857 filed July 9, 1937, noW Patent No. 2,217,639 dated October 8, 1940.

What .I claim as new, and desire to secure by Letters Patent 'of the United States, is:

1. The method of controlling the operation of a fluid heater having a once through flow path, which includes, continuously establishing an electrical impedance value representative of the density of the flowing fluid prior to'heating, continuously establishing an electrical impedance value representative of the density of vthe flowing fluid after heating, averaging the impedances, and utilizing such average in controlling the heating.

2. The method of controlling the operation of a fluid heater having a once through iiow path, which includes, continuously establishing an electrical impedance value representative of the density of the iiowing fluid prior to heating, continuously establishing an electrical impedance value representative of the density of the flowing fluid after heating, 'averaging the impedances, and utilizing such average in controlling the rate of uid ow through the path. y 3. The method of controlling the operation of a fluid heater having a once through iioW path, which includes, `continuously establishing an electrical impedance value representative of the density of theflowing fluid prior to heating, continuously establishing an electrical impedance value representative of the density of the owing fluid after heating, averaging the impedances, and utilizing such average in controlling both the heating and the rate of flow lof thek fluid through the path.

4. A control system for a fluid heater having a oncek through flow path, comprising in combination, heating means for the path, a rate of ow meter for the uid at the entrance to the heater, a differential pressure responsive device for the uid at the exit of the heater, an electrical impedance varied bysaid meter, an electrical impedance varied by said device, a balancing impedance automatically moved to a value determining the ratio of said rst two impedances, and control means for the heating means moved with said balancing impedance.

5. A control system for a fluid heater having a once through iiow path and a plurality of heating sections, comprising in combination, heating means for the path, differential pressure producing devices located in said fluid path at the entrance to said heater, at the inlet to said section, and at the outletfrom said section; means associated with each of said devices for measuring the differential pressure, means for transposing each of the measurements into an electrical effect, means for determining the ratio between the electrical effects representative of the magnitudes of the entrance and inlet diierentials, means for determining the ratio between the electrical effects representative of the magnitudes' of the entrance and outlet diierentials, means positioned in accordance with the average of said ratios, and means positioned with said last named means for controlling the heating means.

6. A control ,systemV for a iluidheatcr having a once through now path, comprising in combination, heating means for theA path, a ratev of flow meter for the fluid at the entrance to the heater, a differential pressure responsive device for the fluid at the exit of the heater, an electrical impedance varied by said meter, an electrical impedance varied by said device, a balancing impedance automatically moved to a value determining the ratio of said first two mpedances, and control means for varying the rate of flow of fluid through the path and moved with said balancing impedance.

7. A control system for a fluid heater having a once through flow path, comprising in combination, heating means for the path, a rate of flow meter for the fluid at the entrance to the heater, a differential pressure responsive device for the il'uid at the exitr of the heater, an electrical impedance varied by said meter, an electrical impedance varied by said device, a balancing impedance automatically moved to a value determining the ratio of said first two impedances, and control means for both varying the rate of flow of fluid through the path and for varying the heating means and moved with said balancing impedance.

8. A control system for a fluid treating system having a once` through fluid flow path, comprising in combination, means for treating the fluid as it flows through the system, a rate of flow meter for the fluid at the entrance to the treating zone, a differential pressure responsive device for the fluid at the exit of the treating zone, an electrical impedance varied by said meter, an electrical impedance varied by said device, a balancingimpedance,automatically moved to a value determining the ratio of said'rst two impedances, and air actuated control means for the treating means moved with said balancing impedance.

9. A control system for a fluid treating system having a once through fluid flow path, comprising in combination, means for treating the fluid as it flows through the system, a differential pressure responsive device for the fluid. flow at the entrance to the treating zone, a second differential pressure responsive d'evice for the fluid flow at the exit ofthe treating zone, an electrical impedance varied by said rst device to a value representative ofthe rst differential pressure, an electrical impedance varied by said second device to a value representative ol" the second differential pressure, a balancing impedance automatically moved to a value determining the ratio of said first two impedances, and control means for the treating means moved with said balancing impedance.

10. The method of controlling the operation of a fluid heater havingV a once through flow path, which includes, establishing electrical impedance values each representative of a variable condition of the flowing fluid, continuously interrelating such values and thereby determining an electrical impedance value representative of the density of the flowing fluid as it is being heated, utilizing such determined. value in ascertaining the density of the fluid as it is being heated', establishing an optimum density for the fluid, and so controlling the heating by the use of the ascertained actual density of the iluid as to maintain the desired optimum density.

ll. The method of controlling the operation of a fluid heater having a once through flow path, which includes, establishing electrical impedance values each representative of. a. variable condition of the flowing fluid, continuously interrelating such values and thereby establishing an electrical impedance value representative of the density of the flowing fluid as it is being heated, establishing an optimum density for the fluid, and so controlling the heating by the use of the established actual electrical impedance value as to maintain the desired optimum density.

12. The method of. operating a fluid heat exchanger having a forced circulation path, which includes, establishing electrical impedance values each representative of a variable condition of the flowing fluid, continuously interrelating such values and thereby establishing an electrical irnpedance value representative of the in situ density of the flowing fluid as it leaves the heat exchanger, establishing an optimum density for the fluid leaving the heat exchanger, and so controlling the heat exchanger by use of the established actual electrical impedance value as to maintain the density of the fluid leaving the heat exchanger at the desired optimum value.

13. The method of operating a fluid treating system having a once through flow path, which includes, establishing electrical impedance values each representative of. a variable condition of the flowing fluid, continuously interrelating such values and thereby establishing an electrical impedance value representative of the density of the flowing fluid as it is being treated, establishing an optimum density for the fluid', and so controlling the treatment' by the use of the established actual electrical. impedance value as to maintain the desired optimum density.

14. The method of operating a fluid treating system having a once through fluid flow path, which includes, establishing electrical impedance values each representative of a variable condition of the flowing fluid, continuously interrlating such values and thereby establishing an electrical impedance value representative of the density of the flowing fluid as it is being treated, establishing an optimum heat content fo-r the fluid leaving the treating zone, and so controlling the heat content by the use of the established actual electrical impedance value as to maintain the desired. optimum heat content.

l5. The method of operating a fluid treating system having a once through fluid flow path, which includes, establishing electrical impedance values each representativeof a variablecondition of the flowing fluid, continuously interrelating such values and therebyl determining an electrical impedance value representative of the density of the flowing fluidas it is being treated, utilizing such determined, value in ascertaining the density of the lluid as it isy being treated, establishing an optimum heat content for the fluid leaving the treating zone, and so controlling the heat content by use of the ascertained actual density of the fluid as to maintain thefdesired optimum heat content.

16. The method of operating a fluid treating system having a once through flow path, which includes, establishing electrical impedance values each representative of a variable condition of the flowing fluid, continuously interrelating such values and thereby establishing. an electrical impedance value representative ofthe density of the flowing fluid as it is beingv treated, establishing an optimum density for the. fluid, and so controlling the rate of fluid. flow through the path by the use of the established. actual electrical impedance value as to maintain the desired optimum density. v*

17. The method of operating a fluid treating system having a once through flow path, which includes, heating the fluid as it passes through the system, establishing electrical impedance values each representative of a variable condition of the flowing fluid, continuously interrelating such values and thereby establishing an electrical impedance value representative of the density of the flowing fluid as it is being treated, establishing an optimum density for the fluid, and so controlling both the rate of fluid flow through the path and the heating by the use of the established actual electrical impedance value as to maintain the desired optimum density.

18. A control system for a fluid heater having a once through ow path, including in combination, heating means for the path, a diierential pressuure responsive device for the uid at the entrance to the heater, a diierential pressure responsive device for the iiuid at the exit of the heater, an electrical impedance varied by each of said devices, a balancing impedance automatically moved to a value determining the ratio of said first two impedances, and control means for the heating means moved with said balancing impedance.

19. A control system for a fluid heater having a once through flow path, including in combination, heating means for the path, a differential pressure responsive device for the iiuid at the entrance to the heater, a differential pressure responsive device for the fluid at the exit of the heater, an electrical impedance varied by each of said devices, a balancing impedance automatically moved to a value determining the ratio of said first two impedances, and control means for the rate of iluid ow through the path moved with said balancing impedance.

20. A control system for a fluid heater having a once through ilow path, including in combination, heating means for the path, a differential pressure responsive device for the fluid at the entrance to the heater, a differential pressure responsive device for the fluid at the exit of the heater, an electrical impedance varied by each of said devices, a balancing impedance automatically moved to a value determining the ratio of said first two impedances, and control means for both the heating means and for the rate of fluid ow through the path moved with said balancing impedance.

21. A control system for a forced circulation fluid heater, including in combination, heating means for the heater, separate means each positioned representative of a variable condition of the fluid before and after heating, an electrical impedance varied by each of said separate means, means continuously interrelating said electrical impedances and thereby establishing an effect representative of the in situ density of the fluid leaving the heater, and control means for the heating means moved with said interrelating means.

22. A control system for a forced circulation fluid heater, including in combination, heating means for the heater, separate means each positioned representative of a variable condition of the fluid before and after heating, an electrical impedance varied by each of said separate means, means continuously interrelating said electrical impedances and thereby establishing an effect representative of the in situ density of the iluid leaving the heater, and control means for the rate of fluid flow through the heater moved with said interrelating means.

23. A control system for a forced circulation iiuid heater, including in combination, heating means for the heater, separate means each positioned representative of a variable condition of the fluid before and after heating, an elec-trical impedance varied by each of said separate means, means continuously interrelating said electrical impedances and thereby establishing an effect representative of the in situ density of the fluid leaving the heater, and control means for both the heating means and the rate of fluid flow through the path moved with said interrelating means.

JOHN F. LUHRS.

v CERTIFICATE oF CORRECTION. Patent No. 2,286,865. June I6, `191g.

JOHN F. LUHRS. v

It is hereby Certified that errorappears in the printed specification of the above numbered patent requiring correction as follows; Page 5,

firstl column, line 2h., for "mdlSzRate of flow (lbs. per unit-TY' read --resistance; andthat the said' Letters Patent should be read with this correction therein that the same may Conform to the record 'of the case in,

the Patent Office. v

Signed and sealed this 25th' day of August, A. D. 1914.2.

Henry Van Arsdale,

(Seal) Acting Commissioner ofv Patents. 

